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AR104069A1 - Proceso integrado de deshidrogenación de hidrocarburos c₃₋₄ - Google Patents

Proceso integrado de deshidrogenación de hidrocarburos c₃₋₄

Info

Publication number
AR104069A1
AR104069A1 ARP160100806A ARP160100806A AR104069A1 AR 104069 A1 AR104069 A1 AR 104069A1 AR P160100806 A ARP160100806 A AR P160100806A AR P160100806 A ARP160100806 A AR P160100806A AR 104069 A1 AR104069 A1 AR 104069A1
Authority
AR
Argentina
Prior art keywords
catalyst
hydrocarbon feed
partially deactivated
deactivated
product
Prior art date
Application number
ARP160100806A
Other languages
English (en)
Inventor
T Pretz Matthew
Original Assignee
Dow Global Technologies Llc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Dow Global Technologies Llc filed Critical Dow Global Technologies Llc
Publication of AR104069A1 publication Critical patent/AR104069A1/es

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    • C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
    • C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
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    • C07C5/3332—Catalytic processes with metal oxides or metal sulfides
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Abstract

Reivindicación 1: Un proceso integrado para producir olefinas C₃₋₄ o di-olefinas C₃₋₄ que comprende los pasos de: (1) (a) contactar, en un reactor de deshidrogenación fluidizado, (i) una alimentación de hidrocarburo C₃₋₄ y (ii) una alimentación de catalizador que comprende un catalizador que cumple los requerimientos de una clasificación Geldart A o Geldart B; en una proporción de alimentación de catalizador respecto de la alimentación de hidrocarburo C₃₋₄ de 5 a 100 sobre la base de peso en peso; donde opcionalmente la alimentación de hidrocarburo C₃₋₄ y la suministro del catalizador se precalentaron a una temperatura de aproximadamente 400ºC a aproximadamente 660ºC; y donde el tiempo promedio de contacto entre la alimentación de hidrocarburo C₃₋₄ y la suministro del catalizador es de aproximadamente 1 segundo a aproximadamente 10 segundos; y donde la temperatura de reacción en el reactor de deshidrogenación fluidizado es de aproximadamente 550ºC a aproximadamente 750ºC; y donde la presión en el reactor de deshidrogenación fluidizado es de 6,0 a 44,7 libras por pulgada cuadrada absoluta en la salida del reactor; en condiciones tales que se forma una mezcla del producto del paso (1)(a), que comprende una olefina o di-olefina C₃₋₄ meta, hidrógeno y alimentación de hidrocarburo C₃₋₄ sin reaccionar; y sobre el catalizador se ha depositado coque y está al menos parcialmente desactivado de modo que forma un catalizador al menos parcialmente desactivado; y (b) transferir la mezcla del producto del paso (1) (a) y el catalizador al menos parcialmente desactivado desde el reactor de deshidrogenación fluidizado a un sistema de separación ciclónico, y opcionalmente enfriar la mezcla del producto del paso (1) (a) y el catalizador al menos parcialmente desactivado a una temperatura inferior a la temperatura de reacción, produciéndose tal enfriamiento antes, después o ambos antes y después, de la transferencia de la misma al sistema de separación ciclónica; en condiciones tales que (i) la mezcla del producto del paso (1) (a) y el catalizador al menos parcialmente desactivado permanecen en contacto a la temperatura de reacción y después de la transferencia al sistema de separación ciclónica, durante un tiempo promedio de 0 segundos a menos que aproximadamente 10 segundos, y (ii) la mezcla del producto del paso (1) (a) es convertida para formar una mezcla de producto del paso (1) (b); y después de ello separar sustancialmente la mezcla de producto del paso (1) (b) y el catalizador al menos parcialmente desactivado uno de otro; (c) transferir al menos una porción del catalizador al menos parcialmente desactivado a un recipiente regenerador y calentar el catalizador al menos parcialmente desactivado allí a una temperatura de combustión de aproximadamente 660ºC a aproximadamente 850ºC a fin de combustionar el coque depositado sobre el catalizador al menos parcialmente desactivado allí, usando el calor generado por la misma combustión de coque y también por un combustible suplementario, formando el calentamiento un catalizador calentado, desactivado adicionalmente que presenta una actividad para deshidrogenar la alimentación de hidrocarburo C₃₋₄ que es menor que aquella del catalizador al menos parcialmente desactivado, y (d) someter el catalizador calentado, desactivado adicionalmente a un paso de acondicionamiento, que comprende mantener el catalizador calentado, desactivado adicionalmente a una temperatura de al menos 660ºC bajo un flujo de gas que contiene oxígeno durante más de 2 minutos, para formar un catalizador al menos parcialmente reactivado que contiene oxígeno que presenta una actividad para deshidrogenar la alimentación de hidrocarburo C₃₋₄ que es mayor que aquel del catalizador al menos parcialmente desactivado; y (e) transferir el catalizador al menos parcialmente reactivado de regreso al reactor de deshidrogenación fluidizado; (2) transferir la mezcla de producto del paso (1) (b) a un compresor, donde la mezcla de producto del paso (1) (b) es comprimida al menos una vez para formar una mezcla del producto del paso (2); y (3) transferir la mezcla del producto del paso (2) a un área de recuperación de producto, donde la mezcla del producto del paso (2) es separada en productos recuperados que comprende al menos una o más fracciones de olefina o di-olefina C₃₋₄ meta, y opcionalmente, una o más fracciones adicionales seleccionadas de una fracción de una alimentación de hidrocarburo C₃₋₄ sin reaccionar; una fracción gaseosa liviana; una fracción de pesados; una fracción de productos secundarios; y combinaciones de las mismas; y donde opcionalmente al menos una porción de la fracción opcional de la alimentación de hidrocarburo C₃₋₄ sin reaccionar se recicla para retornar al paso (1) (a); y donde opcionalmente uno o más de los productos recuperados es transferido a una segunda unidad de recuperación de producto y el paso (3) de separación es repetido allí; y donde opcionalmente la fracción gaseosa liviana opcional es transferida al paso (1) (c) para usarse como el combustible suplementario.
ARP160100806A 2015-03-30 2016-03-23 Proceso integrado de deshidrogenación de hidrocarburos c₃₋₄ AR104069A1 (es)

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